CN105349193A - Method for making methane-enriched gas in low-temperature and heat exchange mode - Google Patents
Method for making methane-enriched gas in low-temperature and heat exchange mode Download PDFInfo
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- CN105349193A CN105349193A CN201510909039.XA CN201510909039A CN105349193A CN 105349193 A CN105349193 A CN 105349193A CN 201510909039 A CN201510909039 A CN 201510909039A CN 105349193 A CN105349193 A CN 105349193A
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Abstract
The invention belongs to the technical field of coal chemical industries and relates to a method for making methane-enriched gas through industrial emission gas containing carbon and hydrogen, in particular to a method for making methane-enriched gas in a low-temperature and heat exchange mode. The method includes the following steps that 1, the pressure of raw material gas is raised to 0.5-3.5 Mpa through a compressor, and the raw material gas is purified, so that total sulfur is smaller than 0.1*10<6> mg/Nm<3>; 2, the raw material gas, steam and recycled gas are mixed and then enter a single-level low-temperature heat exchange methanation reactor, and a heat insulation catalyst layer is arranged at the position, below a column tube, of the reactor; 3, part of a byproduct, namely 5.0 MPa-10.0 MPa steam of methanation enters the reactor. According to the method, through process design of a low-temperature heat exchange single-level methanation reaction and performance improvement of the catalyst, the problem is solved, meanwhile the service life of the catalyst synthesized by methane is well prolonged, the utilization rate of energy is raised, device investment is effectively lowered, and the method can be used for industrial production of making substitute natural gas through carbon and hydrogen industrial emission gas.
Description
Technical field
The invention belongs to technical field of coal chemical industry, relate to containing hydrocarbon industrial discharge gas high methane gas method, be specially a kind of method of low-temperature heat exchange high methane gas.
Background technology
China is the producing country such as first coal, coke, iron and steel, cement, yellow phosphorus, calcium carbide, Coal Chemical Industry, chlor-alkali in the world, discharges CO every year
2more than 70 hundred million tons, the hundreds of billion cubic meter of methane, yellow phosphoric tail gas etc. is containing the tens billion of cubic meter of CO industrial gaseous waste and hundreds billion of cubic metres of organic exhaust gas.
And manyly in these industrial discharge gas have the component of recovery value to be not yet utilized effectively; A large amount of objectionable impuritiess (as sulphur, phosphorus, arsenic, fluorine, NOx, VOCs, dust etc.) enters air simultaneously, causes the serious wasting of resources and environmental pollution.
CO, CO in coal gas is referred to containing the methanation of hydrocarbon industrial discharge gas
2and H
2cH is generated under certain temperature, pressure and catalyst action
4reaction.Principal reaction is as follows:
As can be seen from above-mentioned reaction formula, methanation reaction is strong exothermal reaction, and for coke(oven)gas, the thermal insulation warming often transforming 1%CO is about 63 DEG C, often transforms 1%CO
2thermal insulation warming be about 50.5 DEG C, exothermic heat of reaction amount is quite large.Low temperature can make methanation reaction carry out to positive dirction, thus reaction heat must be removed, and reactor catalyst bed is carried out at the temperature of gentleness, avoids the knot carbon risk of overtemperature in methanation operating process and methanation catalyst.
The current application containing hydrocarbon industrial discharge gas, particularly coke(oven)gas has made great progress, but obtains industrialization success and run good mainly adiabatic methanation process, but flow process is comparatively complicated, need arrange the methanation of 2-4 level; Adiabatic reactor generally all adopts refractory liner simultaneously, and thickness is comparatively large, is also connected with follow-up heat-exchange equipment waste heat boiler simultaneously, adds subsequent installation and dismantlement work amount; Higher to the heat resistant requirements of catalyzer.
Also have at present the research of low-temperature heat exchange high methane gas, but all there is technique and move heat not in time, reactor burns out and the problem such as sintering of catalyst, exports CO simultaneously
2more difficultly reach technic index requirement, chemical process need be adopted to remove CO
2.Do not arrange recycle compressor, although the energy consumption of reducing, save compressor investment, the adaptability that technique fluctuates to unstripped gas is poor, is difficult to realize the effective control to bed temperature.
Wherein for coke(oven)gas, as can be seen from the composition of coke(oven)gas, H wherein
2, CH
4, CnHm and CO be most valuable industrial chemicals, therefore on the basis that large quantity research and engineering development are put into practice, propose a kind of method of low-temperature heat exchange high methane gas, and high methane gas can be separated further, the clean energy Sweet natural gas that production China is in short supply.By the adjustment of processing parameter and the improvement of methanator, greatly reduce the possibility of beds temperature runaway, make the CO+CO of synthesis system
2amount more easily regulate, provide a kind of and can solve the methanation reaction device smooth running in different hydrocarbon industrial discharge gas source and the technic index of methanation.
Summary of the invention
The object of the invention is to for above technical problem, a kind of method of low-temperature heat exchange high methane gas is provided, the method can solve that the flow process that exists in prior art is complicated, heat-exchange equipment is many and the problem such as energy consumption of compressor is high, and solve existing low-temperature heat exchange technique methanation reaction low conversion rate by the improvement of technique, methanation outlet CO
2can not transform completely, avoid the problem of follow-up increase decarbonization device.
The object of the invention is realized by following technical proposals:
A method for low-temperature heat exchange high methane gas, the method comprises the following steps:
1) unstripped gas by compressor boost to 0.5-3.5MPa, and by purification after make total sulfur be less than 0.1 × 10
-6mg/Nm
3.
2) methanation: adopt single-stage low-temperature heat exchange methanator, wherein reactor arranges adiabatic catalyst layer under tubulation, obtains the high methane gas based on methane.
The unstripped gas temperature entering low-temperature heat exchange methanator is 250-350 DEG C, and temperature out is 300-380 DEG C.
3) process steam of methanation by-product 5.0MPa-10.0MPa, the part in process steam and unstripped gas are mixed to join in reactor, and the volume ratio of process steam and unstripped gas is 0.05-0.2.
The volume ratio of internal circulating load and unstripped gas is 0-0.5; recycle compressor adjustment circulating flow rate can be set according to the requirement of the composition of unstripped gas and gas product; this is conducive to, when unstripped gas fluctuation is larger (mend carbon technology), controlling temperature of reaction, protective reaction equipment and catalyzer.
The methanation catalyst adopted is nickel system methanation catalyst, nickel is the catalyzer of active constituent, this catalyzer has good low temperature active under high-speed condition, in tubulation, catalyzer adopts ￠ 3.5mm × 3.5mm (diameter × height) cylinder shape or the circular ring type of ￠ 6mm (diameter) with centre hole (aperture is 2.5mm), adiabatic catalytic oxidant layer adopts ￠ 10-16mm (diameter) irregular shape catalyst with 5 holes (aperture is 2mm), and catalyzer operation air speed is 6000-15000h
-1, technic index is better than traditional method.
The application solves gas distribution inequality by the improvement of methanator and moves hot limited in one's ability and cause the localized hyperthermia of reactor to damage and sintering of catalyst.Methanator lower cover place arranges adiabatic catalytic oxidant layer, reaction compartment increases, and take full advantage of the space of reactor, under equal space velocities, output can increase about 15%, while saving complete assembly investment, efficiently solve the problem of methanation process index.
The application is by entering compressor boost to 0.5-3.5MPa by unstripped gas, qualified and total sulfur is less than 0.1 × 10 from front end purification
-6mg/Nm
3unstripped gas with water vapor and pass into the single-stage methanator that methanation catalyst is housed after mixing from the circulation gas of methanator.Adiabatic catalytic oxidant layer is set after shell-and-tube reactor, effectively can improves methanation reaction transformation efficiency and guarantee to export CO
2be less than 50ppm.Methanator is worked off one's feeling vent one's spleen temperature 300-380 DEG C, after entering reactor charge heating, own temperature drops to about 160 DEG C, then by after preheat boiler-feed-water, de-salted water, after circulating water, gas product is divided into two portions again, a part is as circulation gas noted earlier, and another part sends battery limit (BL).
By the flow scheme design of low-temperature heat exchange single-stage methanation reaction and the improvement in performance of catalyzer, while solving the problem, also achieve preferably and extend the methane synthesizing catalyst life-span, improve the utilization ratio of the energy and effectively reduce plant investment, can be used for the industrial production that hydrocarbon industrial discharge gas system substitutes Sweet natural gas.
Positively effect of the present invention is:
(1) the method is passed through, adopt single-stage methanator simple flow, unstripped gas enters beds, adiabatic catalytic oxidant layer is added under tubulation, effectively reduce bed temperature of reaction, promote the carrying out of methanation reaction, the methanation catalyst adopted is nickel system methanation catalyst, this catalyzer has good low temperature active under high-speed condition, can ensure CO, CO
2outlet is less than 50ppm, and chemical process need not be adopted to remove CO
2, technic index is better than traditional method.
(2) methanation service temperature is reduced, provide one can solve high concentration CO+CO
2(mend carbon technology) methanation operation and methanation overtemperature risk, can enhanced process to unstripped gas fluctuation adaptability and better move heat.
(3) mode by adding steam and circulation gas controls reactor outlet temperature, reduces the possibility of catalyst carbon deposition and reactor drawing crack, improves the operation stability of device.
(4) methanator lower cover place arranges adiabatic catalytic oxidant layer, reaction compartment increases, and take full advantage of the space of reactor, under equal space velocities, output can increase about 15%, while saving complete assembly investment, efficiently solve the problem of methanation process index.
(5) in methanator shell, coolant circulating absorbs the heat that in tube side, methanation reaction produces, control the temperature of reaction process in tube layer, control milder methanation reaction, avoid reactor outlet temperature too high, improve the transformation efficiency of CO, decrease the quantity of high temperature service, reduce selection and through engineering approaches difficulty that high temperature brings simultaneously, reduce investment, decrease occupation of land.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the method for low-temperature heat exchange high methane gas described in the embodiment of the present invention 1.
Fig. 2 is the process flow diagram of the method for low-temperature heat exchange high methane gas described in the embodiment of the present invention 2.
Embodiment
All features disclosed in this specification sheets, or the step in disclosed all methods or process, except mutually exclusive feature and/or step, all can combine by any way.
Arbitrary feature disclosed in this specification sheets (comprising any accessory claim, summary), unless specifically stated otherwise, all can be replaced by other equivalences or the alternative features with similar object.That is, unless specifically stated otherwise, each feature is an example in a series of equivalence or similar characteristics.
Embodiment 1:
Hydrocarbon industrial discharge gas in this technique, it produces because its composition of difference of raw material sources and technique etc. also has certain difference, and several frequently seen is as shown in table 1 with shown in table 2 containing hydrocarbon industrial discharge gas typical case composition.
Table 1 typical case is containing hydrocarbon industrial discharge gas 1 butt composition
Table 2 typical case is containing hydrocarbon industrial discharge gas 2 butt composition
| Title | H 2 | CO | CO 2 | N 2 | CH 4 | O 2 |
| Content V% | 28.0 | 50.0 | 6.0 | 14.0 | 1.5 | 0.5 |
Containing most valuable industrial chemicals in its composition, should be utilized further.The technique means realized to make the present invention, inventive features, reach object and effect is easy to understand, giving an actual example below describes the present invention.
Embodiment 1:
The method of low-temperature heat exchange high methane gas, idiographic flow schematic diagram is with reference to figure 1, and adopting containing hydrocarbon industrial discharge gas 1 is raw material, and tolerance 1000kmol/h, temperature is 40 DEG C.Unstripped gas 1 through purify qualified after total sulfur≤0.1 × 10
-6mg/Nm
3, butt mainly forms, and (vol%) is: CH
4: 24.91, H
2: 56.40, CO:9.13, CO
2: 3.32, C
2h
6: 2.50, C
3h
8: 0.11, N
2: 3.63, total vol% is 100%, tolerance 963.4kmol/h.Its (H
2-CO
2)/(CO+CO
2) mol ratio be 4.26, as methanation unstripped gas.
Unstripped gas is at pressure 2.5MPa, and temperature in enters methanation device under being about the condition of 250 DEG C.Qualified and total sulfur≤0.1 × 10 from front end purification
-6mg/Nm
3unstripped gas mix with water vapor after pass into the single-stage methanator that methanation catalyst is housed.Thermal insulation layer catalyst layer is set after shell-and-tube reactor, methanator temperature of working off one's feeling vent one's spleen is about 380 DEG C, after entering reactor charge heating, own temperature drops to about 165 DEG C, then by preheat boiler-feed-water, after de-salted water, then after circulating water 40 DEG C send battery limit (BL) as gas product.
The steam part that methanation produces joins in reactor, and the volume ratio of process steam and unstripped gas is about 0.1; The shell side top steam water interface of methanator enters the steam pockets at its top, the saturation steam of 10.0MPa is produced after being separated, boiling water in drum goes back to again the shell side bottom of reactor according to gravity circulation, form a gravity circulation loop, constantly remove methanation reaction heat, maintain methanation and carry out in a mild condition.Produce 10.0MPa saturation steam in reaction process and be about 8.0t/h, recycle gas compressor power consumption is 0, and recirculated water consumption is about 47t/h, and outlet CO concentration is lower than 5ppm, CO
2concentration is lower than 50ppm.
The methanation catalyst adopted is nickel system methanation catalyst, nickel is the catalyzer of active constituent, this catalyzer has good low temperature active under high-speed condition, in tubulation, catalyzer adopts ￠ 3.5mm × 3.5mm (diameter × height) cylinder shape or the circular ring type of ￠ 6mm (diameter) with centre hole (aperture is 2.5mm), adiabatic catalytic oxidant layer adopts ￠ 10-16mm (diameter) irregular shape catalyst with 5 holes (aperture is 2mm), and catalyzer operation air speed is 6000-15000h
-1, the 2-5 being current isothermal process air speed doubly, is 1-3 times of adiabatic technique air speed, CO transformation efficiency 99%, CO
2transformation efficiency 99%, technic index is better than traditional method.
Methanator lower cover place arranges adiabatic catalytic oxidant layer, and ensure the index of methanation process, under equal space velocities, output can increase about 15%, saves an adiabatic reactor and follow-up interchanger and water cooler or chemical treatment CO
2device.
Embodiment 2:
The method of low-temperature heat exchange high methane gas, idiographic flow schematic diagram is with reference to figure 2, and adopting containing hydrocarbon industrial discharge gas 1 is raw material, and tolerance 1000kmol/h, temperature is 40 DEG C.Supplementary carbon source tolerance 20kmol/h, it mainly forms, and (vol%) is: CO
2: 98.5, N
2: 1.50, temperature is 40 DEG C.Unstripped gas 1 and supplementary carbon source through purify qualified after total sulfur≤0.1 × 10
-6mg/Nm
3, butt mainly forms, and (vol%) is: CH
4: 24.41, H
2: 55.26, CO:8.95, CO
2: 5.26, C
2h
6: 2.45, C
3h
8: 0.08, N
2: 3.59, total vol% is 100%, tolerance 963.4kmol/h.Its (H
2-CO
2)/(CO+CO
2) mol ratio be 3.52, as methanation unstripped gas.
Unstripped gas is at pressure 3.5MPa, and temperature in is about 280 DEG C and enters methanation device.Qualified and total sulfur≤0.1 × 10 from front end purification
-6mg/Nm
3unstripped gas with water vapor and pass into the single-stage methanator that methanation catalyst is housed after mixing from the circulation gas of methanator.Thermal insulation layer catalyst layer is set after shell-and-tube reactor, methanator temperature of working off one's feeling vent one's spleen is about 300 DEG C, after entering reactor fresh feed gas and circulation gas preheating, own temperature drops to about 130 DEG C, then by after preheat boiler-feed-water/de-salted water, after circulating water to 40 DEG C, gas product is divided into two portions again, and a part is as circulation gas noted earlier, and another part sends battery limit (BL).
The steam part that methanation produces joins in reactor, and the volume ratio of process steam and synthetic gas is about 0.05; Adopt reciprocation compressor, compressor inlet temperature 40 DEG C, can reduce the addition of process steam, and the volume ratio of internal circulating load and fresh feed gas is 0.44.The shell side top steam water interface of methanator enters the steam pockets at its top, 5.0MPa saturation steam is produced after being separated, boiling water in drum goes back to again the shell side bottom of reactor according to gravity circulation, form a gravity circulation loop, constantly remove methanation reaction heat, maintain methanation and carry out in a mild condition.Produce 5.0MPa saturation steam in reaction process and be about 10.0t/h, recycle gas compressor power consumption is about 21kwh, and recirculated water consumption is about 66t/h, and outlet CO concentration is lower than 5ppm, CO
2concentration is lower than 50ppm.And traditional single stage shell-and-tube reactor outlet CO
2concentration is greater than 100ppm, need set up chemical process and take off CO
2device or connect a set of adiabatic methanation device and supporting heat-exchange system.Control reactor outlet temperature by the mode adding steam and circulation gas, reduce the drawing crack possibility of catalyst carbon deposition and reactor, improve the operation stability of device.
The methanation catalyst adopted is nickel system methanation catalyst, nickel is the catalyzer of active constituent, this catalyzer has good low temperature active under high-speed condition, in tubulation, catalyzer adopts ￠ 3.5mm × 3.5mm (diameter × height) cylinder shape or the circular ring type of ￠ 6mm (diameter) with centre hole (aperture is 2.5mm), adiabatic catalytic oxidant layer adopts ￠ 10-16mm (diameter) irregular shape catalyst with 5 holes (aperture is 2mm), and catalyzer operation air speed is 6000-15000h
-1, the 2-5 being current isothermal process air speed doubly, is 1-3 times of adiabatic technique air speed, CO transformation efficiency 99%, CO
2transformation efficiency 99%, technic index is better than traditional method.
Methanator lower cover place arranges adiabatic catalytic oxidant layer, and ensure the index of methanation process, under equal space velocities, output can increase about 15%, saves an adiabatic reactor and follow-up interchanger and water cooler or chemical treatment CO
2device.
Embodiment 3:
Fig. 1 is the method for low-temperature heat exchange high methane gas, and adopting containing hydrocarbon industrial discharge gas 2 is raw material, and tolerance 1000kmol/h, temperature is 40 DEG C.Unstripped gas 2 through conversion decarburization and purify qualified after total sulfur≤0.1 × 10
-6mg/Nm
3, butt mainly forms, and (vol%) is: CH
4: 2.75, H
2: 57.75, CO:9.17, CO
2: 4.67, N
2: 25.66, total vol% is 100%, tolerance 545.5kmol/h, its (H
2-CO
2)/(CO+CO
2) mol ratio be 3.83, as methanation unstripped gas.
Unstripped gas is at pressure 1.0MPa, and temperature in is enter methanation device under 300 DEG C of conditions.Qualified and total sulfur≤0.1 × 10 from front end purification
-6mg/Nm
3unstripped gas mix with water vapor after pass into the single-stage methanator that methanation catalyst is housed.Thermal insulation layer catalyst layer is set after shell-and-tube reactor, methanator temperature of working off one's feeling vent one's spleen is about 340 DEG C, after entering reactor gas mixture and changing preheating, own temperature drops to about 138 DEG C, then by preheat boiler-feed-water, after de-salted water, then after circulating water 40 DEG C send battery limit (BL) as gas product.
The steam part that methanation produces joins in reactor, and the volume ratio of process steam and unstripped gas is about 0.15; The shell side top steam water interface of methanator enters the steam pockets at its top, the saturation steam of 5.0MPa is produced after being separated, boiling water in drum goes back to again the shell side bottom of reactor according to gravity circulation, form a gravity circulation loop, constantly remove methanation reaction heat, maintain methanation and carry out in a mild condition.Produce 5.0MPa saturation steam in reaction process and be about 5.0t/h, recycle gas compressor power consumption is 0, and recirculated water consumption is about 34t/h, and outlet CO concentration is lower than 1ppm, CO
2concentration is lower than 50ppm.
The methanation catalyst adopted is nickel system methanation catalyst, nickel is the catalyzer of active constituent, this catalyzer has good low temperature active under high-speed condition, in tubulation, catalyzer adopts ￠ 3.5mm × 3.5mm (diameter × height) cylinder shape or the circular ring type of ￠ 6mm (diameter) with centre hole (aperture is 2.5mm), adiabatic catalytic oxidant layer adopts ￠ 10-16mm (diameter) irregular shape catalyst with 5 holes (aperture is 2mm), and catalyzer operation air speed is 6000-15000h
-1, the 2-5 being current isothermal process air speed doubly, is 1-3 times of adiabatic technique air speed, CO transformation efficiency 99%, CO
2transformation efficiency 99%, technic index is better than traditional method.
Methanator lower cover place arranges adiabatic catalytic oxidant layer, and ensure the index of methanation process, under equal space velocities, output can increase about 15%, saves an adiabatic reactor and follow-up interchanger and water cooler or chemical treatment CO
2device.
The present invention is not limited to aforesaid embodiment.The present invention expands to any new feature of disclosing in this manual or any combination newly, and the step of the arbitrary new method disclosed or process or any combination newly.
Claims (5)
1. a method for low-temperature heat exchange high methane gas, is characterized in that comprising the following steps:
1) unstripped gas by compressor boost to 0.5-3.5MPa, and by purification after make total sulfur be less than 0.1 × 10
-6mg/Nm
3;
2) unstripped gas enters single-stage low-temperature heat exchange methanator after mixing with steam and circulation gas, and wherein reactor arranges adiabatic catalyst layer under tubulation;
3) steam of the 5.0MPa-10.0MPa of methanation by-product, a part of steam joins in reactor.
2. the method for low-temperature heat exchange high methane gas according to claim 1, is characterized in that: the unstripped gas temperature entering low-temperature heat exchange methanator is 250-350 DEG C, and after reaction, temperature out is 300-380 DEG C.
3. the method for low-temperature heat exchange high methane gas according to claim 1, is characterized in that: step 2) described in steam and the volume ratio of unstripped gas be 0.05-0.2.
4. the method for low-temperature heat exchange high methane gas according to claim 1, is characterized in that: step 2) described in circulation gas and the volume ratio of unstripped gas be 0-0.5.
5. the method for low-temperature heat exchange high methane gas according to claim 1, it is characterized in that: step 2) described in the methanation catalyst that adopts of adiabatic catalytic oxidant layer be nickel system methanation catalyst, this catalyzer has good low temperature active under high-speed condition, in tubulation, catalyzer adopts ￠ 3.5mm × 3.5mm cylinder shape or ￠ 6mm to be with the circular ring type of centre hole, adiabatic catalytic oxidant layer adopts the irregular shape catalyst of ￠ 10-16mm, and catalyzer operation air speed is 6000-15000h
-1.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101812339A (en) * | 2010-04-15 | 2010-08-25 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas, and natural gas product thereof |
| CN101880559A (en) * | 2010-06-18 | 2010-11-10 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
| CN102250658A (en) * | 2010-05-19 | 2011-11-23 | 上海标氢气体技术有限公司 | Method for preparing liquefied natural gas by converting raw materials of coke oven gas and blast furnace gas |
| KR20120033081A (en) * | 2010-09-29 | 2012-04-06 | 현대제철 주식회사 | Hydrogen and methane gas producing device using two phase anaerobic digestion reactor |
| CN204247177U (en) * | 2014-11-24 | 2015-04-08 | 成都赛普瑞兴科技有限公司 | A kind of thermal insulation-isothermal methanation reactor |
-
2015
- 2015-12-10 CN CN201510909039.XA patent/CN105349193A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101812339A (en) * | 2010-04-15 | 2010-08-25 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas, and natural gas product thereof |
| CN102250658A (en) * | 2010-05-19 | 2011-11-23 | 上海标氢气体技术有限公司 | Method for preparing liquefied natural gas by converting raw materials of coke oven gas and blast furnace gas |
| CN101880559A (en) * | 2010-06-18 | 2010-11-10 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
| KR20120033081A (en) * | 2010-09-29 | 2012-04-06 | 현대제철 주식회사 | Hydrogen and methane gas producing device using two phase anaerobic digestion reactor |
| CN204247177U (en) * | 2014-11-24 | 2015-04-08 | 成都赛普瑞兴科技有限公司 | A kind of thermal insulation-isothermal methanation reactor |
Non-Patent Citations (1)
| Title |
|---|
| 林玉波等: "《合成氨生产工艺》", 28 February 2006 * |
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